CN101089145A - Petroleum hydrocarbon treating process - Google Patents
Petroleum hydrocarbon treating process Download PDFInfo
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- CN101089145A CN101089145A CN 200610046934 CN200610046934A CN101089145A CN 101089145 A CN101089145 A CN 101089145A CN 200610046934 CN200610046934 CN 200610046934 CN 200610046934 A CN200610046934 A CN 200610046934A CN 101089145 A CN101089145 A CN 101089145A
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Abstract
The process of producing clean fuel with petroleum hydrocarbons has well combined hydrocracking process, hydrodesulfurizing process, catalytically cracking process and coking process. It has most of decompressed wax oil from crude oil desulfurized and catalytically cracked, the coked wax oil obtained through coking catalytically cracked tail oil and vacuum residual oil hydrocracked, and the hydrocracked tail oil catalytically cracked for the second time. The combined process can obtain petroleum coke product, high quality hydrocracked light oil product and catalytically cracked light oil product simultaneously. Facilitate the operation of hydrocracking apparatus, increase the service life of the catalyst and obtain clean fuel in high economic benefit.
Description
Technical field
The present invention relates to a kind of working method of producing clean fuel, specifically, relate to a kind of novel process that coking technology, hydrogenating desulfurization technology, hydrocracking technology combine with catalytic cracking technology by petroleum hydrocarbon.
Background technology
Along with the increasingly stringent of expanding economy in the world wide and environmental regulation, the demand and the quality product of petroleum products all there is stricter requirement.Simultaneously, worldwide crude oil becomes heavy, variation day by day, brings bigger difficulty to processing.
Existing crude oil work flow is generally, the light-end products that atmospheric and vacuum distillation unit comes out directly mix (or through refining back) with other device gained light-end products and directly dispatch from the factory, decompressed wax oil enters hydroeracking unit, obtain high grade light-end products and high-quality tail oil, as described in JP11012578, US4834865 and US5164514 etc.Depressed heavy oil enters coker or catalytic cracking unit, and/or behind the residual hydrogenation upgrading, enter catalytic cracking unit again, obtain products such as relatively poor light ends of character and coke, and the relatively poor light ends of these character can not conform to the requirement of high quality cleaning product after directly cut mixes preferably with character.Therefore the relatively poor cut of these character must through could directly dispatch from the factory after refining (it is refining to be generally medium-pressure hydrocracking) or mix with other corresponding cuts after dispatch from the factory, as FR2764902, RU2058371, US5068025 and US5068025 etc. are described.Although catalytic cracking process along with the development of technology, all improves in every respect and innovates, still there is increasing problem in use separately.In existing catalytic cracking and the hydrocracking combined process, its flow process is carried out catalytic cracking for the long residuum with crude oil, the purpose product is a gasoline, LCO in the reaction product and HCO (light, heavy cycle oil) mix with the normal pressure intermediate oil and carry out hydrocracking, hydrocracking tail oil or circulation or enter catalytic cracking or the oil that acts as a fuel, catalytically cracked oil effluxes, as described in US4426276 and US3193488 etc.It is relatively poor that the subject matter of this technology is that long residuum carries out the gasoline product quality that catalytic cracking obtains, and can't satisfy the environmental requirement of increasingly stringent, and simultaneously along with the intermediate oil demand obviously increases, this technical process then needs further to improve.And this technology is not comprehensively determined the adjustment of its feedstock property at the characteristics of different device, does not give full play to the advantage of different device.In addition, because refinery's treatment capacity increases, and the heavy crude amount increases, so also corresponding increase of output heavy, residual oil, this makes the development of means of this important light materialization of heavy oil of catalytic cracking be subjected to limiting significantly, need to improve the quality product of catalytic cracking unit, reduce its operating severity with other method.
Summary of the invention
At the deficiencies in the prior art, the object of the present invention is to provide a kind ofly will weigh, method that residual oil is processed as the high-quality light oil products, the inventive method can be converted into light oil products to greatest extent with heavy, residual oil, and the quality product height, intermediate oil yield height.
The inventive method comprises: the vacuum residuum of (1) crude oil carries out coking to be handled, and wax tailings carries out hydrocracking; (2) the decompressed wax oil part of crude oil is carried out hydrogenating desulfurization, and the desulfurization after product carries out catalytic cracking, and the catalytic cracking tail oil carries out hydrocracking; (3) decompressed wax oil another part of crude oil carries out hydrocracking, and hydrocracking tail oil carries out the raw material of catalytic cracking or conduct production lubricant base.The part by weight that the decompressed wax oil of crude oil advances hydrogenating desulfurization and advances hydrocracking is 1: 5～10: 1, preferred 5: 1～1: 1.Wherein hydrocracking can comprise the hydrogenation pre-refining, oil type hydrocracking catalyst during hydrocracking is preferred.Decompressed wax oil most of or all carry out hydrogenating desulfurization in order to adjust the operation of each device, also can partly enter the hydrocracking system.The raw material sources that carry out hydrocracking are in decompressed wax oil, catalytic cracking tail oil and wax tailings, and the mixed weight ratio is 0～5: 0.1～5: 0.1: 5.
Compared with prior art, characteristics of the present invention are: hydrocracking technology, the hydrogenating desulfurization technology, the organic combination of catalytic cracking technology and coking technology, the advantage that has promptly kept hydroeracking unit to produce high grade light-end products, the eco-friendly lightweight high-quality of direct production hydrocracking product, the mixing oil of hydrocracking tail oil and a part of decompressed wax oil (or all) after hydrogenating desulfurization as the catalytic cracking unit charging, make the charging quality of catalytic cracking unit improve the corresponding device operating severity that reduced greatly, prolonged the work-ing life of catalytic cracking catalyst, increase the total liquid yield of catalytic cracking, coke and reacted gas productive rate have been reduced, heavy feed stock lighting rate is improved greatly, and can obtain the quite low catalytic cracking light ends oil of sulphur content, meet the requirement of environmental protection to petroleum products, but also can production part refinery coke product, realized the reasonable utilization of petroleum resources like this, substantially can realize refinery's " zero " discharging, for the refinery increases very big economic benefit.The characteristics of the inventive method integrated catalytic cracking, hydrocracking, coker, determined work flow heavy, residual oil, promptly brought into play the advantage of different device, improved the clean or white yield simultaneously, and improved quality product, can be used for all kinds refinery and be used for handling heavy, residual oil.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Embodiment
As shown in Figure 1, crude oil 1 enters atmospheric unit 2 and reliever 5 after refining plant (not identifying on the figure) purifying treatment, obtain various straight run light ends oil 3 and 6 and depressed heavy oil 7, depressed heavy oil and turning oil 13 enter coker 8, obtain refinery coke and coking and generate oil 9, wherein coking generates oil 9 and obtain coking vapour in coking fractional distillation column 10, diesel oil distillate 11 and wax tailings 12 and turning oil 13, wax tailings 12 mixes the back with catalytic cracking tail oil 20 and part decompressed wax oil and enters hydrofining reactor 21 with hydrogen 28, obtain hydrofining and generate oil 22, it enters hydrocracking reactor 23 with hydrogen 28, hydrocracking generates oil 24 and separates in hydrocracking separation column 25, obtain hydrocracking gas, vapour, coal, diesel oil distillate 26 and hydrocracking tail oil 27, hydrocracking tail oil 27 can all enter catalytic cracking unit, also can be with a part wherein 29 as base oil of high viscosity index lubricant.Part in the decompressed wax oil 30 (or all) and hydrogen 28 enter hydrodesulphurisatioreactors reactors 14, obtain sweet oil 15, its with enter catalytic cracking unit 16 after hydrocracking tail oil 27 mixes, the catalytic cracking full distillate oil 17 of generation obtains catalyzer cracked gas, vapour, diesel oil distillate 19 and catalytic cracking tail oil 20 in catalytic fractionator 18.The decompressed wax oil of crude oil advances hydrogenating desulfurization and advances the part by weight of hydrocracking, can adjust by the working ability of quality product requirement and device.
Operational condition to each device is described below below.
Coking is a raw material with heavy, residual oil mainly, can obtain light-end products and wax tailings such as coking vapour, diesel oil, coking technology has the coking of still formula, open hearth coking, delayed coking, contact coking and fluid coking etc. several, and relatively commonly used have delayed coking and a fluid coking.The process using delayed coking technology of this patent, with vacuum residuum as raw material, be heated to 480～600 ℃ of temperature ins, best 500～550 ℃, enter coke drum, carry out cracking, condensation reaction, generate coke, oil gas fractionation in separation column that reaction generates obtains gas, gasoline, diesel oil and wax oil and turning oil, and turning oil loops back coke drum.
Hydrocracking technology is the indispensable important means of modern refineries production high-quality clean fuel, can be divided into three kinds by work flow: two-stage method flow process, one-stage serial flow process and method by single-stage flow process.Wherein in the two-stage method work flow in second section reactor the catalyzer of adorning mostly be noble metal catalyst, can maximum obtain the high-quality light-end products, generally adopt extinction recycle operation.The characteristics of traditional method by single-stage flow process are less investments, but raw material is limited to some extent, and the improvement flow process of method by single-stage (the two agent technologies of single hop) is wider to raw material subject range.The one-stage serial flow process comprises hydrofining section and hydrocracking section, but between do not have sepn process.Preferred one-stage serial flow process of the inventive method and method by single-stage flow process.
The one-stage serial flow process comprises hydrofining reactor, hydrocracking reactor and hydrogenation fractionating tower three parts.Wherein Hydrobon catalyst in the reactor and hydrocracking catalyst, they all are made up of carrier and the hydrogenation metal that is loaded in above it, with the weight percent is benchmark, hydrogenation metal is a base metal, comprise the group vib active metal component, as tungsten and/or molybdenum, count 10%～35% with metal oxide, 15～30% is better; And the group VIII reactive metal, as nickel and/or cobalt, count 1%～7% with metal oxide, 1.5%～6% is better.The carrier that Hydrobon catalyst uses is an inorganic refractory oxide, as aluminum oxide, amorphous silicon aluminium, silicon oxide, titanium oxide etc., commercial Hydrobon catalyst mainly contains: the HC-K of Uop Inc., HC-T, HC-P, 3936,3996 of Fushun Petrochemical Company catalyst plant, FF-16, FF-26 etc. that Fushun Petrochemical Research Institute produces.The carrier of hydrocracking catalyst is aluminum oxide and molecular sieve, molecular sieve content is generally 20%～60%, commercial hydrocracking catalyst mainly contains: the HC-12 of Uop Inc., HC-14, FC-12, the FC-14 of 3976,3974,3971 and Fushun Petrochemical Research Institute's development and production of Fushun Petrochemical Research Institute's development Fushun Petrochemical Company catalyst plant, FC-16, FC-24, FC-26 etc.Catalyzer layering filling has cold hydrogen hand-hole between each bed, inject cold hydrogen during operation, takes away the reaction heat that hydrogenation reaction and cracking reaction produce, and makes temperature of reaction within the specific limits, makes operation safe, steady.Described hydrofining reactor operational condition is: pressure is 5.0MPa～19.0MPa, best 10.0 MPa～16.0MPa; Average reaction temperature is 300 ℃～440 ℃, best 350 ℃～420 ℃; Volume space velocity 0.1h during liquid
-1～3.0h
-1, best 0.4h
-1～2.0h
-1Hydrogen to oil volume ratio is 100: 1～3000: 1, best 500: 1～2000: 1.The hydrofining reactor outlet is refining to generate oily organonitrogen content less than 200 μ g/g, preferably less than 100 μ g/g.The logistics of coming out from hydrofining reactor can be used or without intermediate separator the hydrogen sulfide that generates and ammonia and low boiler cut be separated, and enters hydrocracking reactor then.Described hydrocracking reactor operational condition is: pressure is 5.0MPa～19.0MPa, preferably 10.0MPa～16.0MPa; Average reaction temperature is 300 ℃～440 ℃, best 350 ℃～420 ℃; Volume space velocity 0.1h during liquid
-1～3.0h
-1, best 0.4h
-1.8h
-1Hydrogen to oil volume ratio is 100: 1～3000: 1, best 500: 1～2000: 1.But product and hydrocracking tail oils such as described hydrogenation fractionating tower direct production liquefied gas, light naphthar, heavy naphtha, aviation kerosene, diesel oil, the yield of hydrocracking tail oil is 10wt%～80wt%, preferably 20wt%～50wt%.Hydrocracking tail oil sulphur nitrogen content is less than 200 μ g/g, and the BMCI value is less than 30, and preferably the sulphur nitrogen content is less than 50 μ g/g, and the BMCI value is less than 25.
The hydrodesulphurisatioreactors reactors and the hydrofining reactor of technology of the present invention are similar, main purpose is most sulphur and the most of the nitrogen that removes in the stock oil, wherein sulphur and nitrogen transformation are hydrogen sulfide and ammonia, the catalyzer that it uses is made up of carrier and the hydrogenation metal that is loaded in above it, with the weight percent is benchmark, hydrogenation component comprises group vib active metal component (as tungsten and/or molybdenum), counts 10%～30% with metal oxide, and 15～25% is better; Group VIII active metal component (as nickel and/or cobalt), count 1%～7% with metal oxide, 1.5%～6% is better, carrier is aluminum oxide or siliceous aluminum oxide etc., the FDS-4 that commercial catalysts such as Wenzhou catalyst plant are produced, the FF-14 of Fushun Petrochemical Research Institute's development and production, FF-18 etc.Operational condition: pressure is 5.0MPa～19.0MPa, preferably 8.0MPa～16.0MPa; Average reaction temperature is 300 ℃～440 ℃, best 330 ℃～420 ℃; Volume space velocity 0.1h during liquid
-1～3.0h
-1, best 0.4h
-1～2.0h
-1Hydrogen to oil volume ratio is 100: 1～3000: 1, best 500: 1～2000: 1.The hydrodesulphurisatioreactors reactors outlet generates oily organic sulfur content less than 1500 μ g/g, and is better less than 800 μ g/g, preferably less than 500 μ g/g.
Catalytic cracking technology is a most important course of processing in the crude oil secondary processing, but quality product is not high, does not meet the requirement of the environmental regulation of increasingly stringent.For improving the catalytic cracking quality product, technology of the present invention is taked to realize with the method for other device material cooperation, adjustment charging.Technology catalytically cracked material of the present invention comprises crude oil decompressed wax oil and the hydrocracking tail oil through hydrogenating desulfurization.Catalytic cracking unit comprises catalyst cracker and catalytic fractionator two portions.The operational condition of catalyst cracker is: 450 ℃～550 ℃ of average reaction temperature, best 480 ℃～520 ℃; Agent weight of oil ratio is 2～30, best 3～20; With catalyzer duration of contact be 0.5 second～15 seconds, best 0.5 second～5 seconds; Reaction pressure is 0.1～0.5MPa, best 0.1～0.3MPa.Catalytic fractionator can be produced low-density oil cut or product and catalytic cracking tail oils such as liquefied gas, light naphthar, heavy naphtha, aviation kerosene, diesel oil, wherein the yield of catalytic cracking tail oil is 10wt%～80wt%, and preferably yield is 30wt%～60wt%.
Consider coker, hydroeracking unit, hydrodesulfurization unit and catalytic cracking unit are united use, with former catalytic cracking tail oil part and the wax tailings that is used as catalytic cracking turning oil, after mixing, most of decompressed wax oil (or all) and hydrogen enters hydrofining reactor, remove the organic nitrogen compound of the toxic effect of hydrocracking catalyst to less than behind the 100 μ g/g, enter hydrocracking reactor, hydrogenation through a series of complexity, cracking reaction, the hydrocracking mixing oil that obtains is divided into all kinds of light-end productss and (comprises gas products in the hydrogenation fractionating tower, gently, heavy naphtha, boat coal and diesel oil) and hydrogenation tail oil, hydrocracking tail oil with enter catalyst cracker after the hydrodesulfurization unit sweet oil mixes, generate oil through obtaining catalytic cracking behind the catalytic cracking reaction, it is divided into all kinds of light-end productss and (comprises gas products in catalytic fractionator, gasoline and diesel oil) and the catalytic cracking tail oil, the catalytic cracking tail oil, wax tailings and a part of decompressed wax oil enter the inlet of hydroeracking unit, form operate continuously.
Below by embodiment the present invention program and effect are described.
Embodiment 1～2
Embodiment 1 is different with the crude oil of embodiment 2 processing, and these two kinds of different crude oil enter atmospheric and vacuum distillation unit after refining plant is handled, obtain light ends oil, 350～470 ℃ decompressed wax oil cut and 470 ℃+depressed heavy oil cut.
Wherein 470 ℃
+The depressed heavy oil cut is heated to 520 ℃ and enters coke drum, obtains product and the character thereof listed as following table through after the pyrogenic reaction.
| Embodiment 1 | |
|
| Feedstock property | ||
| Density, g/cm 3 | 0.958 | 0.962 |
| Carbon residue, wt% | 8.3 | 8.5 |
| Sulphur, wt% | 3.0 | 3.3 |
| Product yield and product property | ||
| Gasoline, wt% | 18.0 | 16.5 |
| Diesel oil, wt% | 30.0 | 29.5 |
| Wax oil, wt% | 27.0 | 26.5 |
| Coke, wt% | 18.5 | 20.5 |
| Gas+loss, wt% | 6.5 | 7.0 |
| Gasoline octane rating | 75 | 73 |
| Diesel cetane-number | 36 | 35 |
Embodiment 1 is decompressed wax oil+350 ℃ of 30wt% crude oil
+Catalytic cracking tail oil+wax tailings enters hydroeracking unit, controls 350 ℃
+The transformation efficiency that cut is converted into 350 ℃ of cuts is 60wt%; Embodiment 2 is decompressed wax oil+350 ℃ of 20wt% crude oil
+Catalytic cracking tail oil+wax tailings enters hydroeracking unit, controls 350 ℃
+The transformation efficiency that cut is converted into 350 ℃ of cuts is 60wt%; Feedstock property, processing condition and product property are listed in the table below.Hydrobon catalyst is 3936, and hydrocracking catalyst is 3974.
| Embodiment 1 | |
|||
| Feedstock property | ||||
| Density, g/cm 3 | 0.956 | 0.970 | ||
| Sulphur, wt% | 2.0 | 1.8 | ||
| Nitrogen, wt% | 0.15 | 0.14 | ||
| The reaction stagnation pressure, MPa | 15.7 | 15.7 | ||
| Volume space velocity during liquid, h -1 | (1.0 making with extra care) | (1.5 cracking) | (0.95 making with extra care) | (1.4 cracking) |
| Hydrogen to oil volume ratio | 1000: 1 (making with extra care) | 1500: 1 (cracking) | 1000: 1 (making with extra care) | 1500: 1 (cracking) |
| Average reaction temperature, ℃ | 380 (making with extra care) | 382 (crackings) | 375 (making with extra care) | 380 (crackings) |
| The treated oil nitrogen content, μ g/g | ＜10 | ＜10 | ||
| Product yield and character | ||||
| Gas, wt% | 5.6 | 5.3 | ||
| Petroleum naphtha, wt% | 12.5 | 11.6 | ||
| Rocket engine fuel+diesel oil, wt% | 41.9 | 43.1 | ||
| Tail oil, wt% | 40.0 | 40.0 | ||
| The petroleum naphtha arene underwater content, wt% | 57 | 59 | ||
| Tail oil sulphur+nitrogen, μ g/g | ＜100 | ＜100 | ||
Embodiment 1 is for the decompressed wax oil of 70wt% crude oil enters hydrodesulfurization unit, and embodiment 2 is for the decompressed wax oil of 80wt% crude oil enters hydrodesulfurization unit, and processing condition are listed in the table below, and all obtains the sweet oil that sulphur content is 400 μ g/g.Hydrobon catalyst is FDS-4.
| Embodiment 1 | |
|
| The reaction stagnation pressure, MPa | 15.7 | 15.7 |
| Volume space velocity during liquid, h -1 | 1.3 | 1.5 |
| Hydrogen to oil volume ratio | 800∶1 | 800∶1 |
| Average reaction temperature, ℃ | 380 | 385 |
| The product sulphur content, μ g/g | 400 | 400 |
Two embodiment hydrogenating desulfurizations enter catalytic cracking unit after generating oil and catalytic cracking tail oil mixing post-heating to 500 ℃, control 350 ℃
+Cut is converted into 350 ℃
-The transformation efficiency of cut is 60wt%, and stock oil is listed in the table below with the product and the product property that obtain, and the tail oil of separating enters hydroeracking unit.Catalytic cracking catalyst is the REY catalytic cracking catalyst that Chang Ling oil-refining chemical head factory is produced.
| Embodiment 1 | |
|
| Stock oil character | ||
| Density, g/cm 3 | 0.918 | 0.926 |
| Sulphur, μ g/g | 240 | 280 |
| Nitrogen, μ g/g | 150 | 175 |
| Temperature of reaction, ℃ | 500 | 500 |
| Pressure, MPa | 0.25 | 0.25 |
| Agent-oil ratio, | 15 | 15 |
| Finish duration of contact, s | 3 | 3 |
| Product distributes and product property, wt% | ||
| Gas products | 3.0 | 3.2 |
| Gasoline, wt% | 40.1 | 36.9 |
| Diesel oil, wt% | 13.4 | 16.5 |
| Tail oil, wt% | 40.0 | 40.0 |
| Coke, wt% | 3.5 | 3.4 |
| Content of sulfur in gasoline, μ g/g | 170 | 180 |
| The diesel oil sulphur content, μ g/g | 220 | 230 |
| The tail oil carbon residue, wt% | ＜1.0 | ＜1.0 |
By two embodiment as can be seen, use this patent technology to carry out crude oil processing, can obtain high-quality hydrocracking product, satisfy the catalytic cracking light-end products of environmental requirement, finally obtain clean fuel, can also obtain the refinery coke product.
Claims (9)
1, a kind of petroleum hydrocarbon working method comprises following step mule: the vacuum residuum of (1) crude oil carries out coking to be handled, and wax tailings carries out hydrocracking; (2) the decompressed wax oil part of crude oil is carried out hydrogenating desulfurization, and the desulfurization after product carries out catalytic cracking, and the catalytic cracking tail oil carries out hydrocracking; (3) decompressed wax oil another part of crude oil carries out hydrocracking, and hydrocracking tail oil carries out the raw material of catalytic cracking or conduct production lubricant base.
2, in accordance with the method for claim 1, it is characterized in that described hydrocracking is the one-stage serial hydrocracking that comprises hydrofining and hydrocracking, or be single-stage hydrocracking.
3, in accordance with the method for claim 1, it is characterized in that the described raw material sources that carry out hydrocracking in decompressed wax oil, catalytic cracking tail oil and wax tailings, the mixed weight ratio is 0～5: 0.1～5: 0.1: 5.
4, in accordance with the method for claim 1, it is characterized in that described coking is delayed coking.
5, according to claim 1 or 4 described methods, it is characterized in that described coking product obtains gas, gasoline, diesel oil and wax oil and turning oil through the separation column fractionation, turning oil loops back coke drum.
6, in accordance with the method for claim 2, it is characterized in that described hydrofining reactor operational condition is: pressure is 5.0MPa～19.0MPa, and temperature of reaction is 300 ℃～440 ℃, volume space velocity 0.1h during liquid
-1～3.0h
-1, hydrogen to oil volume ratio is 100: 1～3000: 1, the hydrofining reactor outlet is refining to generate oily organonitrogen content less than 200 μ g/g; Described hydrocracking reactor operational condition is: pressure is 5.0MPa～19.0MPa, and temperature of reaction is 300 ℃～440 ℃, volume space velocity 0.1h during liquid
-1～3.0h
-1, hydrogen to oil volume ratio is 100: 1～3000: 1, and the yield of hydrocracking tail oil is 10wt%～80wt%, and hydrocracking tail oil sulphur nitrogen content is less than 200 μ g/g, and the BMCI value is less than 30.
7, in accordance with the method for claim 1, it is characterized in that described hydrogenating desulfurization operational condition is: pressure is 5.0MPa～19.0MPa, and temperature of reaction is 300 ℃～440 ℃, volume space velocity 0.1h during liquid
-1～3.0h
-1, hydrogen to oil volume ratio is 100: 1～3000: 1, the hydrodesulphurisatioreactors reactors outlet generates oily organic sulfur content less than 1500 μ g/g.
8, in accordance with the method for claim 1, the operational condition that it is characterized in that described catalytic cracking is: 450 ℃～550 ℃ of temperature of reaction, agent weight of oil ratio is 2～30, with catalyzer duration of contact be 0.5 second～15 seconds, reaction pressure is 0.1～0.5MPa, the yield of catalytic cracking tail oil is 10wt%～80wt%, and preferably yield is 3 0wt%～60wt%.
9, in accordance with the method for claim 1, the decompressed wax oil that the it is characterized in that described crude oil part by weight that advances hydrogenating desulfurization and advance hydrocracking is 1: 5～10: 1.
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